NOx ADSROBER CATALYST

ABSTRACT

A NO x  adsorber catalyst composition, a NO x  adsorber catalyst and its use in an emission treatment system for internal combustion engines, is disclosed. The NO x  adsorber catalyst composition a support material and one or more platinum group metals disposed on the support material, wherein the support material comprises a mixed dopant NO x  storage enhancer.

FIELD OF THE INVENTION

The invention relates to a NO_(x) adsorber catalyst composition, a NO_(x) adsorber catalyst comprising the composition, and emission systems for internal combustion engines comprising the NO_(x) adsorber catalyst.

BACKGROUND OF THE INVENTION

Internal combustion engines produce exhaust gases containing a variety of pollutants, including nitrogen oxides (“NO_(x)”), carbon monoxide, and uncombusted hydrocarbons, which are the subject of governmental legislation. Increasingly stringent national and regional legislation has lowered the amount of pollutants that can be emitted from such diesel or gasoline engines. Emission control systems are widely utilized to reduce the amount of these pollutants emitted to atmosphere, and typically achieve very high efficiencies once they reach their operating temperature (typically, 200° C. and higher). However, these systems are relatively inefficient below their operating temperature (the “cold start” period).

One exhaust gas treatment component utilized to clean exhaust gas is the NO_(x) adsorber catalyst (or “NO_(x) trap”). NO_(x) adsorber catalysts are devices that adsorb NO_(x) under lean exhaust conditions, release the adsorbed NO_(x) under rich conditions, and reduce the released NO_(x) to form N₂. A NO_(x) adsorber catalyst typically includes a NO_(x) adsorbent for the storage of NO_(x) and an oxidation/reduction catalyst.

The NO_(x) adsorbent component is typically an alkaline earth metal, an alkali metal, a rare earth metal, or combinations thereof. These metals are typically found in the form of oxides. The oxidation/reduction catalyst is typically one or more noble metals, preferably platinum, palladium, and/or rhodium. Typically, platinum is included to perform the oxidation function and rhodium is included to perform the reduction function. The oxidation/reduction catalyst and the NO_(x) adsorbent are typically loaded on a support material such as an inorganic oxide for use in the exhaust system.

The NO_(x) adsorber catalyst performs three functions. First, nitric oxide reacts with oxygen to produce NO₂ in the presence of the oxidation catalyst. Second, the NO₂ is adsorbed by the NO_(x) adsorbent in the form of an inorganic nitrate (for example, BaO or BaCO₃ is converted to Ba(NO₃)₂ on the NO_(x) adsorbent). Lastly, when the engine runs under rich conditions, the stored inorganic nitrates decompose to form NO or NO₂ which are then reduced to form N₂ by reaction with carbon monoxide, hydrogen and/or hydrocarbons (or via NH_(x) or NCO intermediates) in the presence of the reduction catalyst. Typically, the nitrogen oxides are converted to nitrogen, carbon dioxide and water in the presence of heat, carbon monoxide and hydrocarbons in the exhaust stream.

Typically, NO_(x) adsorbent materials consist of inorganic oxides such as alumina, silica, ceria, zirconia, titania, or mixed oxides which are coated with at least one platinum group metal. PCT Intl. Appl. WO 2008/047170 discloses a system wherein NO_(x) from a lean exhaust gas is adsorbed at temperatures below 200° C. and is subsequently thermally desorbed above 200° C. The NO_(x) adsorbent is taught to consist of palladium and a cerium oxide or a mixed oxide or composite oxide containing cerium and at least one other transition metal.

PCT Intl. Appl. WO 2004/076829 discloses an exhaust-gas purification system which includes a NO_(x) storage catalyst arranged upstream of an SCR catalyst. The NO_(x) storage catalyst includes at least one alkali, alkaline earth, or rare earth metal which is coated or activated with at least one platinum group metal (Pt, Pd, Rh, or Ir). A particularly preferred NO_(x) storage catalyst is taught to include cerium oxide coated with platinum and additionally platinum as an oxidizing catalyst on a support based on aluminium oxide. EP 1027919 discloses a NO_(x) adsorbent material that comprises a porous support material, such as alumina, zeolite, zirconia, titania, and/or lanthana, and at least 0.1 wt % precious metal (Pt, Pd, and/or Rh). Platinum carried on alumina is exemplified.

NO_(x) adsorber catalysts are typically exposed to cyclic oxidizing and reducing conditions. During the oxidizing cycle, NO_(x) is stored on the catalyst. During the reducing cycle, NO_(x) is released and/or reduced (e.g. to N₂). It is well known in the art (Applied Catalysis B: Environmental 5 (1995) 367-376) that certain catalysts, such as platinum on ceria (Pt—CeO₂), can be activated by a reduction pre-treatment. However, such activation can only be achieved above a relatively high temperature, and is reversed after re-oxidation pre-treatment.

At low temperatures (typically below about 200° C.), the NO_(x) storage function of these catalysts is inefficient and continues to be an area of catalyst development in need of improvement. It is also desirable for catalysts to be developed that have little or no NO_(x) storage properties at greater than a specific temperature, to allow control of when NO_(x) is released for subsequent conversion by, for example, a further downstream catalyst.

As with any automotive system and process, it is desirable to attain still further improvements in exhaust gas treatment systems. We have discovered a new NO_(x) adsorber catalyst composition with improved low temperature NO_(x) storage characteristics, and improved NOx release properties.

It has surprisingly been found that NO_(x) adsorber catalyst compositions comprising platinum group metals on a support that is doped with a mixture of certain metals or metal oxides have improved low temperature NO_(x) storage properties, and which, in certain embodiments, are more readily activated by reduction pre-treatment and retain this activation after exposure to oxidizing conditions.

SUMMARY OF THE INVENTION

In a first aspect of the invention there is provided a NOx adsorber catalyst composition comprising a support material and one or more platinum group metals disposed on the support material; wherein the one or more platinum group metals is selected from the group consisting of palladium, platinum, or a mixture or alloy of platinum and palladium; wherein the support material comprises alumina, ceria, a ceria/zirconia mixed or composite oxide, or a magnesia/alumina mixed or composite oxide; and wherein the support material comprises a mixed dopant NOx storage enhancer, wherein the mixed dopant NOx storage enhancer comprises a plurality of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof.

In a second aspect of the invention there is provided a NO_(x) adsorber catalyst comprising the NO_(x) adsorber catalyst composition as hereinbefore defined supported on a metal or ceramic substrate.

In a third aspect of the invention there is provided a NO_(x) adsorber catalyst comprising the NO_(x) adsorber catalyst composition as hereinbefore defined, wherein the catalyst composition is extruded to form a flow-through or filter substrate.

In a fourth aspect of the invention there is provided an emission treatment system for internal combustion engines comprising the NO_(x) adsorber catalyst as hereinbefore defined.

In a fifth aspect of the invention there is provided a method of treating an exhaust gas from an internal combustion engine comprising contacting the exhaust gas with the NO_(x) adsorber catalyst as hereinbefore defined.

In an sixth aspect of the invention there is provided the use of a mixed dopant NO_(x) storage enhancer to improve the low temperature NO_(x) storage capacity of a support material, relative to an equivalent support material that does not contain the mixed dopant NO_(x) storage enhancer.

In an seventh aspect of the invention there is provided the use of a mixed dopant NOx storage enhancer to improve the NOx reduction activity of a support material during a rich purge, relative to an equivalent support material that does not contain the mixed dopant NOx storage enhancer.

In an eighth aspect of the invention there is provided the use of a mixed dopant NO_(x) storage enhancer to improve the N₂ selectivity of a support material during a rich purge, relative to an equivalent support material that does not contain the mixed dopant NOx storage enhancer.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows NO_(x) concentration at 250° C. during a cyclic lean-rich condition test of samples aged at 800° C.

FIG. 2 shows NO_(x) concentration at 150° C. during a cyclic lean-rich condition test of samples aged 800° C. and subsequently reduced at 300° C.

DEFINITIONS

The term “washcoat” is well known in the art and refers to an adherent coating that is applied to a substrate, usually during production of a catalyst.

The acronym “PGM” as used herein refers to “platinum group metal”. The term “platinum group metal” generally refers to a metal selected from the group consisting of Ru, Rh, Pd, Os, Ir and Pt, preferably a metal selected from the group consisting of Ru, Rh, Pd, Ir and Pt. In general, the term “PGM” preferably refers to a metal selected from the group consisting of Rh, Pt and Pd.

The term “mixed oxide” as used herein generally refers to a mixture of oxides in a single phase, as is conventionally known in the art. The term “composite oxide” as used herein generally refers to a composition of oxides having more than one phase, as is conventionally known in the art.

The expression “substantially free of” as used herein with reference to a material means that the material in a minor amount, such as 5% by weight, preferably 2% by weight, more preferably 1% by weight. The expression “substantially free of” embraces the expression “does not comprise”.

DETAILED DESCRIPTION OF THE INVENTION

The invention relates to A NOx adsorber catalyst composition comprising a support material and one or more platinum group metals disposed on the support material; wherein the one or more platinum group metals is selected from the group consisting of palladium, platinum, or a mixture or alloy of platinum and palladium; wherein the support material comprises alumina, ceria, a ceria/zirconia mixed or composite oxide, or a magnesia/alumina mixed or composite oxide; and wherein the support material comprises a mixed dopant NOx storage enhancer, wherein the mixed dopant NOx storage enhancer comprises a plurality of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof.

The mixed dopant NO_(x) storage enhancer comprises a plurality (i.e. more than one, e.g. two or more) of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof.

The mixed dopant NO_(x) storage enhancer can comprise a plurality of, e.g. more than one of, any salt, oxide, complex or other compound that contains the elements listed above.

The mixed dopant NO_(x) storage enhancer may be present on the surface of the support material. The mixed dopant NO_(x) storage enhancer may, additionally or alternatively, be incorporated into the support material. One example of the mixed dopant NO_(x) storage enhancer being incorporated into the support material would be the replacement of atoms of the support material by atoms of components of the mixed dopant NO_(x) storage enhancer, e.g. in the lattice structure of the support material.

Preferably the support material is doped with the mixed dopant NO_(x) storage enhancer.

The mixed dopant NO_(x) storage enhancer comprises a plurality of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof. For the avoidance of doubt, the mixed dopant NO_(x) storage enhancer may comprise more than one different element selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof.

In some embodiments, the mixed dopant NO_(x) storage enhancer preferably comprises samarium, or a salt, oxide, complex or other compound thereof, in combination with at least one different rare earth metal, one or more alkali earth metals, or mixtures thereof, and/or metal oxides thereof.

Preferably the mixed dopant NO_(x) storage enhancer is selected from a mixture of neodymium and samarium, gadolinium and praseodymium, lanthanum and samarium, lanthanum and strontium, samarium and strontium, calcium and strontium, or magnesium and strontium, or metal oxides thereof. For the avoidance of doubt, these are merely examples of preferred mixtures of elements and do not constitute an exhaustive list of all possibilities encompassed by the invention.

In one preferred embodiment of the invention, the mixed dopant NO_(x) storage enhancer comprises a mixture of neodymium and samarium, or metal oxides thereof. For example, the mixed dopant NO_(x) storage enhancer may preferably comprise a mixture of Nd₂O₃ and Sm₂O₃. It has surprisingly been found that this combination of dopants results in a NO_(x) adsorber catalyst composition that has particularly high NO_(x) storage activity over a wide temperature window.

The mixed dopant NO_(x) storage enhancer can be present in the NO_(x) adsorber catalyst composition any amount, but is preferably present in an amount of about 0.5-20 mol %, more preferably about 2-18 mol %, still more preferably about 5-16 mol %, expressed as a total mol % of all of the components of the mixed dopant NO_(x) storage enhancer in the NO_(x) adsorber catalyst composition. For example, the mixed dopant NO_(x) storage enhancer may be present in about 0.5, 1, 2, 4, 6, 8, 10, 12, 14, 16, 18 or 20 mol %.

The mixed dopant NO_(x) storage enhancer components may be present in any relative ratio to each other.

In embodiments wherein the mixed dopant NO_(x) storage enhancer comprises a mixture of two metals or metal oxides, the two different metals or metal oxides may be present in any relative ratio. Preferably, the two different metals or metal oxides are present in a ratio of from 1:10 to 10:1, expressed in terms of mol %. More preferably the two different metals or metal oxides are present in a ratio of from 1:3 to 3:1, expressed in terms of mol %. In some preferred embodiments wherein the mixed dopant NO_(x) storage enhancer comprises a mixture of two metals or metal oxides, the two different metals or metal oxides are present in a 1:1 ratio, expressed in terms of mol %.

One preferred embodiment of the invention therefore comprises a NO_(x) adsorber catalyst composition comprising a mixed dopant NO_(x) storage enhancer which comprises a plurality (i.e. more than one, e.g. two or more) of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof in a ratio of from 1:10 to 10:1, preferably in a ratio of from 1:3 to 3:1, and especially preferably in a ratio of 1:1, all expressed in terms of mol %. One preferred mixed dopant NO_(x) storage enhancer comprises a 1:1 mol % mixture of neodymium and samarium, e.g. a 1:1 mol % mixture of Nd₂O₃ and Sm₂O₃.

One exemplary embodiment of the invention is therefore a NO_(x) adsorber catalyst composition comprising a mixed dopant NO_(x) storage enhancer which comprises 0.5-20 mol %, preferably 2-18 mol %, more preferably 5-16 mol % of a 1:1 mol % mixture of Nd₂O₃ and Sm₂O₃. One particularly preferred embodiment of the invention comprises as the mixed dopant NO_(x) storage enhancer 16 mol % of a 1:1 mol % mixture of Nd₂O₃ and Sm₂O₃.

The support material preferably comprises alumina, ceria, a ceria/zirconia mixed or composite oxide, or a magnesia/alumina mixed or composite oxide. Preferably the support material comprises ceria, e.g. is ceria. In some preferred embodiments, the support material is selected from the group consisting of cerium oxide, a ceria-zirconia mixed oxide, a ceria-magnesia-alumina mixed oxide, and an alumina-ceria-zirconia mixed oxide.

In some embodiments of the invention, the support material further comprises barium. It should be noted, however, that it is not necessary to include barium as a NO_(x) storage material in compositions of the invention, i.e. barium is an optional component of compositions of the invention. In other words, some compositions of the invention are substantially free of barium. Some compositions of the invention are therefore barium-free NO_(x) adsorber catalyst compositions comprising a mixed dopant NO_(x) storage enhancer.

In embodiments where the NO_(x) storage material does comprise barium, a preferred support material is a CeO₂—BaCO₃ composite material. Such a material can be preformed by any method known in the art, for example incipient wetness impregnation or spray-drying. If the NO_(x) adsorber catalyst composition contains barium, the NO_(x) adsorber catalyst composition preferably comprises 0.1 to 10 weight percent barium, and more preferably 0.5 to 5 weight percent barium, e.g. about 4.5 weight percent barium, expressed as a weight % of the composition.

Preferred support materials preferably have a surface area in the range 10 to 1500 m²/g, pore volumes in the range 0.1 to 4 mL/g, and pore diameters from about 10 to 1000 Angstroms. High surface area supports having a surface area greater than 80 m²/g are particularly preferred, e.g. high surface area ceria or alumina. Other preferred support materials include magnesia/alumina composite oxides, optionally further comprising a cerium-containing component, e.g. ceria. In such cases the ceria may be present on the surface of the magnesia/alumina composite oxide, e.g. as a coating.

Compositions of the invention that are substantially free of barium, or do not comprise barium as a NO_(x) storage material (e.g. barium-free NO_(x) adsorber compositions), may be particularly advantageous because they store less NO_(x) at temperatures in excess of 100, 120, 150, 180, 200, 250 or 300° C., preferably about 300° C. than a comparable barium-containing composition. In other words, compositions of the invention that are substantially free of barium, or do not comprise barium as a NO_(x) storage material, have improved NO_(x) release properties at temperatures in excess of 100, 120, 150, 180, 200, 250 or 300° C., preferably about 300° C. than a comparable barium-containing composition. Such compositions may also have improved sulfur tolerance relative to an equivalent barium-containing composition. In this context, “improved sulfur tolerance” means that compositions of the invention that are substantially free of barium are either more resistant to sulfation, can be thermally desulfated at a lower temperature, or both, compared to an equivalent barium-containing composition.

The one or more platinum group metals (PGM) are selected from the group consisting of platinum and palladium, or mixtures thereof. Platinum, palladium and mixtures thereof are particularly preferred, e.g. a mixture of platinum and palladium. The NO_(x) adsorber catalyst composition preferably comprises 0.1 to 10 weight percent PGM, more preferably 0.5 to 5 weight percent PGM, and most preferably 1 to 3 weight percent PGM.

In embodiments wherein the PGM is a mixture of platinum and palladium, the platinum and palladium may be present in any ratio. Preferably, the platinum is present in a greater than 1:1 ratio with the palladium, e.g. 2:1, 3:1, 4:1 or 5:1. In particularly preferred embodiments wherein the PGM is a mixture of platinum and palladium, the platinum:palladium ratio is 2:1 or 5:1, particularly preferably 2:1.

Thus preferably the NOx adsorber catalyst composition comprises, e.g. consists essentially of or consists of, a mixture or alloy of platinum and palladium disposed on a support material, wherein the support material comprises, preferably consists essentially of (e.g. consists of) ceria and a mixed dopant NOx storage enhancer, wherein the mixed dopant NOx storage enhancer comprises a plurality (i.e. more than one, e.g. two or more) of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof, particularly preferably a mixture of neodymium, samarium, or oxides thereof.

The NO_(x) adsorber catalyst composition of the invention may comprise further components that are known to the skilled person. For example, the compositions of the invention may further comprise at least one binder and/or at least one surfactant. Where a binder is present, dispersible alumina binders are preferred.

The NO_(x) adsorber catalyst composition of the present invention may be prepared by any suitable means. Preferably, the one or more platinum group metals, and/or mixed dopant NO_(x) storage enhancer components (i.e. the rare earth metals or rare earth metal oxides, the alkali earth metals or alkali earth metal oxides, or mixtures thereof, or any suitable precursor thereof, e.g. the respective rare earth metal nitrate or alkali earth metal nitrate or mixtures thereof) are loaded onto the support by any known means to form the NO_(x) adsorber catalyst composition. For example impregnation, adsorption, ion-exchange, incipient wetness, precipitation, or the like, or any other means commonly known in the art, may be used. The manner of addition is not considered to be particularly critical.

For example, the support material may be impregnated to incipient wetness with a nitrate precursor of the respective metal oxide(s), dried, and calcinated. The resulting doped support material may then be impregnated with a PGM salt to achieve the desired PGM loading, dried, and calcinated.

The order of addition of the platinum group metal (PGM) and mixed dopant NO_(x) storage enhancer to the support is not considered critical. For example, the PGM and mixed dopant NO_(x) storage enhancer may be added to the support simultaneously, or may be added sequentially in any order. Preferably, however, the mixed dopant NO_(x) storage enhancer is added first, followed by the PGM.

A further aspect of the invention is a NO_(x) adsorber catalyst comprising the NO_(x) adsorber catalyst composition as hereinbefore described supported on a metal or ceramic substrate. The substrate may be a flow-through substrate or a filter substrate, but is preferably a flow-through monolith substrate.

The flow-through monolith substrate has a first face and a second face defining a longitudinal direction therebetween. The flow-through monolith substrate has a plurality of channels extending between the first face and the second face. The plurality of channels extend in the longitudinal direction and provide a plurality of inner surfaces (e.g. the surfaces of the walls defining each channel). Each of the plurality of channels has an opening at the first face and an opening at the second face. For the avoidance of doubt, the flow-through monolith substrate is not a wall flow filter.

The first face is typically at an inlet end of the substrate and the second face is at an outlet end of the substrate.

The channels may be of a constant width and each plurality of channels may have a uniform channel width.

Preferably within a plane orthogonal to the longitudinal direction, the monolith substrate has from 100 to 500 channels per square inch, preferably from 200 to 400. For example, on the first face, the density of open first channels and closed second channels is from 200 to 400 channels per square inch. The channels can have cross sections that are rectangular, square, circular, oval, triangular, hexagonal, or other polygonal shapes.

The monolith substrate acts as a support for holding catalytic material. Suitable materials for forming the monolith substrate include ceramic-like materials such as cordierite, silicon carbide, silicon nitride, zirconia, mullite, spodumene, alumina-silica magnesia or zirconium silicate, or of porous, refractory metal. Such materials and their use in the manufacture of porous monolith substrates is well known in the art.

It should be noted that the flow-through monolith substrate described herein is a single component (i.e. a single brick). Nonetheless, when forming an emission treatment system, the monolith used may be formed by adhering together a plurality of channels or by adhering together a plurality of smaller monoliths as described herein. Such techniques are well known in the art, as well as suitable casings and configurations of the emission treatment system.

In an alternative embodiment of the invention, the NO_(x) adsorber catalyst comprising the NO_(x) adsorber catalyst composition as hereinbefore described is extruded to form a flow-through or filter substrate.

In embodiments wherein the NO_(x) adsorber catalyst comprises a ceramic substrate, the ceramic substrate may be made of any suitable refractory material, e.g., alumina, silica, titania, ceria, zirconia, magnesia, zeolites, silicon nitride, silicon carbide, zirconium silicates, magnesium silicates, aluminosilicates and metallo aluminosilicates (such as cordierite and spodumene), or a mixture or mixed oxide of any two or more thereof. Cordierite, a magnesium aluminosilicate, and silicon carbide are particularly preferred.

In embodiments wherein the NO_(x) adsorber catalyst comprises a metallic substrate, the metallic substrate may be made of any suitable metal, and in particular heat-resistant metals and metal alloys such as titanium and stainless steel as well as ferritic alloys containing iron, nickel, chromium, and/or aluminium in addition to other trace metals.

Preferably, the NO_(x) adsorber catalyst as hereinbefore described is prepared by depositing the NO_(x) adsorber catalyst composition as hereinbefore described on the substrate using washcoat procedures. A representative process for preparing the NO_(x) adsorber catalyst component using a washcoat procedure is set forth below. It will be understood that the process below can be varied according to different embodiments of the invention.

The washcoating is preferably performed by first slurrying finely divided particles of the NO_(x) adsorber catalyst composition in an appropriate solvent, preferably water, to form a slurry. The slurry preferably contains between 5 to 70 weight percent solids, more preferably between 10 to 50 weight percent. Preferably, the particles are milled or subject to another comminution process in order to ensure that substantially all of the solid particles have a particle size of less than 20 microns in an average diameter, prior to forming the slurry. Additional components, such as stabilizers or promoters, may also be incorporated in the slurry as a mixture of water soluble or water-dispersible compounds or complexes.

The substrate may then be coated one or more times with the slurry such that there will be deposited on the substrate the desired loading of the NO_(x) adsorber catalyst composition.

Preferably, the NO_(x) adsorber catalyst comprises a substrate and at least one layer on the substrate. Preferably, the at least one layer comprises the NO_(x) adsorber catalyst composition as hereinbefore described. This can be produced by the washcoat procedure described above. One or more additional layers may be added to the one layer of NO_(x) adsorber catalyst composition.

In embodiments wherein one or more additional layers are present (i.e. in addition to the NO_(x) adsorber catalyst composition), the one or more additional layers have a different composition to the first layer comprising the NO_(x) adsorber catalyst composition.

The one or more additional layers may comprise one zone or a plurality of zones, e.g. two or more zones. Where the one or more additional layers comprise a plurality of zones, the zones are preferably longitudinal zones. The plurality of zones, or each individual zone, may also be present as a gradient, i.e. a zone may not be of a uniform thickness along its entire length, to form a gradient. Alternatively, a zone may be of uniform thickness along its entire length.

In some preferred embodiments, one additional layer, i.e. a second layer, is present.

Typically, the second layer comprises a platinum group metal (PGM) (referred to below as the “second platinum group metal”). It is generally preferred that the second layer comprises the second platinum group metal (PGM) as the only platinum group metal (i.e. there are no other PGM components present in the catalytic material, except for those specified).

The second PGM may be selected from the group consisting of platinum, palladium, and a combination or mixture of platinum (Pt) and palladium (Pd). Preferably, the platinum group metal is selected from the group consisting of palladium (Pd) and a combination or a mixture of platinum (Pt) and palladium (Pd). More preferably, the platinum group metal is selected from the group consisting of a combination or a mixture of platinum (Pt) and palladium (Pd).

It is generally preferred that the second layer is (i.e. is formulated) for the oxidation of carbon monoxide (CO) and/or hydrocarbons (HCs).

Preferably, the second layer comprises palladium (Pd) and optionally platinum (Pt) in a ratio by weight of 1:0 (e.g. Pd only) to 1:4 (this is equivalent to a ratio by weight of Pt:Pd of 4:1 to 0:1). More preferably, the second layer comprises platinum (Pt) and palladium (Pd) in a ratio by weight of <4:1, such as 3.5:1.

When the platinum group metal is a combination or mixture of platinum and palladium, then the second layer comprises platinum (Pt) and palladium (Pd) in a ratio by weight of 5:1 to 3.5:1, preferably 2.5:1 to 1:2.5, more preferably 1:1 to 2:1.

The second layer typically further comprises a support material (referred to herein below as the “second support material”). The second PGM is generally disposed or supported on the second support material.

The second support material is preferably a refractory oxide. It is preferred that the refractory oxide is selected from the group consisting of alumina, silica, ceria, silica alumina, ceria-alumina, ceria-zirconia and alumina-magnesium oxide. More preferably, the refractory oxide is selected from the group consisting of alumina, ceria, silica-alumina and ceria-zirconia. Even more preferably, the refractory oxide is alumina or silica-alumina, particularly silica-alumina.

A particularly preferred second layer comprises a silica-alumina support, platinum, palladium, barium, a molecular sieve, and a platinum group metal (PGM) on an alumina support, e.g. a rare earth-stabilised alumina. Particularly preferably, this preferred second layer comprises a first zone comprising a silica-alumina support, platinum, palladium, barium, a molecular sieve, and a second zone comprising a platinum group metal (PGM) on an alumina support, e.g. a rare earth-stabilised alumina. This preferred second layer may have activity as an oxidation catalyst, e.g. as a diesel oxidation catalyst (DOC).

A further preferred second layer comprises, consists of, or consists essentially of a platinum group metal on alumina This preferred second layer may have activity as an oxidation catalyst, e.g. as a NO₂-maker catalyst.

A further preferred second layer comprises a platinum group metal, rhodium, and a cerium-containing component.

In other preferred embodiments, more than one of the preferred second layers described above are present, in addition to the NO_(x) adsorber catalyst composition. In such embodiments, the one or more additional layers may be present in any configuration, including zoned configurations.

The NO_(x) adsorber catalyst composition may be disposed or supported on the second layer or the substrate (e.g. the plurality of inner surfaces of the through-flow monolith substrate), preferably the second layer is disposed or supported on the NO_(x) adsorber catalyst composition.

The second layer may be disposed or supported on the substrate (e.g. the plurality of inner surfaces of the through-flow monolith substrate).

The second layer may be disposed or supported on the entire length of the substrate or the NO_(x) adsorber catalyst composition. Alternatively the second layer may be disposed or supported on a portion, e.g. 5%, 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%, or 95%, of the substrate or the NO_(x) adsorber catalyst composition.

Preferably, the entire length of the substrate is coated with the NO_(x) adsorber catalyst composition.

A further aspect of the invention is an emission treatment system for treating a flow of a combustion exhaust gas that comprises the NO_(x) adsorber catalyst as hereinbefore described. In preferred systems, the internal combustion engine is a diesel engine, preferably a light duty diesel engine. The NO_(x) adsorber catalyst may be placed in a close-coupled position or in the underfloor position.

The emission treatment system typically further comprises an emissions control device.

The emissions control devices is preferably downstream of the NO_(x) adsorber catalyst. Alternatively, the emissions control device may be upstream of the NO_(x) adsorber catalyst.

Examples of an emissions control device include a diesel particulate filter (DPF), a lean NO_(x) trap (LNT), a lean NO_(x) catalyst (LNC), a selective catalytic reduction (SCR) catalyst, a diesel oxidation catalyst (DOC), a catalysed soot filter (CSF), a selective catalytic reduction filter (SCRF™) catalyst, an ammonia slip catalyst (ASC), a cold start catalyst (dCSC™) and combinations of two or more thereof. Such emissions control devices are all well known in the art.

Some of the aforementioned emissions control devices have filtering substrates. An emissions control device having a filtering substrate may be selected from the group consisting of a diesel particulate filter (DPF), a catalysed soot filter (CSF), and a selective catalytic reduction filter (SCRF™) catalyst.

It is preferred that the emission treatment system comprises an emissions control device selected from the group consisting of a lean NO_(x) trap (LNT), an ammonia slip catalyst (ASC), diesel particulate filter (DPF), a selective catalytic reduction (SCR) catalyst, a catalysed soot filter (CSF), a selective catalytic reduction filter (SCRF™) catalyst, and combinations of two or more thereof. More preferably, the emissions control device is selected from the group consisting of a diesel particulate filter (DPF), a selective catalytic reduction (SCR) catalyst, a catalysed soot filter (CSF), a selective catalytic reduction filter (SCRF™) catalyst, and combinations of two or more thereof. Even more preferably, the emissions control device is a selective catalytic reduction (SCR) catalyst or a selective catalytic reduction filter (SCRF™) catalyst.

When the emission treatment system of the invention comprises an SCR catalyst or an SCRF™ catalyst, then the emission treatment system may further comprise an injector for injecting a nitrogenous reductant, such as ammonia, or an ammonia precursor, such as urea or ammonium formate, preferably urea, into exhaust gas Group VIII transition metals (e.g NO_(x) adsorber catalyst and upstream of the SCR catalyst or the SCRF™ catalyst.

Such an injector may be fluidly linked to a source (e.g. a tank) of a nitrogenous reductant precursor. Valve-controlled dosing of the precursor into the exhaust gas may be regulated by suitably programmed engine management means and closed loop or open loop feedback provided by sensors monitoring the composition of the exhaust gas.

Ammonia can also be generated by heating ammonium carbamate (a solid) and the ammonia generated can be injected into the exhaust gas.

Alternatively or in addition to the injector, ammonia can be generated in situ (e.g. during rich regeneration of a LNT disposed upstream of the SCR catalyst or the SCRF™ catalyst), e.g. a NO_(x) adsorber catalyst comprising the NO_(x) adsorber catalyst composition of the invention. Thus, the emission treatment system may further comprise an engine management means for enriching the exhaust gas with hydrocarbons.

The SCR catalyst or the SCRF™ catalyst may comprise a metal selected from the group consisting of at least one of Cu, Hf, La, Au, In, V, lanthanides and Group VIII transition metals (e.g. Fe, Mn), wherein the metal is supported on a refractory oxide or molecular sieve. The metal is preferably selected from Ce, Fe, Cu and combinations of any two or more thereof, more preferably the metal is Fe or Cu.

The refractory oxide for the SCR catalyst or the SCRF™ catalyst may be selected from the group consisting of Al₂O₃, TiO₂, CeO₂, SiO₂, ZrO₂ and mixed oxides containing two or more thereof. The non-zeolite catalyst can also include tungsten oxide (e.g. V₂O₅/WO₃/TiO₂, WO_(x)/CeZrO₂, WO_(x)/ZrO₂ or Fe/WO_(x)/ZrO₂).

It is particularly preferred when an SCR catalyst, an SCRF™ catalyst or a washcoat thereof comprises at least one molecular sieve, such as an aluminosilicate zeolite or a SAPO. The at least one molecular sieve can be a small, a medium or a large pore molecular sieve. By “small pore molecular sieve” herein we mean molecular sieves containing a maximum ring size of 8, such as CHA; by “medium pore molecular sieve” herein we mean a molecular sieve containing a maximum ring size of 10, such as ZSM-5; and by “large pore molecular sieve” herein we mean a molecular sieve having a maximum ring size of 12, such as beta. Small pore molecular sieves are potentially advantageous for use in SCR catalysts.

In the emission treatment system of the invention, preferred molecular sieves for an SCR catalyst or an SCRF™ catalyst are synthetic aluminosilicate zeolite molecular sieves selected from the group consisting of AEI, ZSM-5, ZSM-20, ERI including ZSM-34, mordenite, ferrierite, BEA including Beta, Y, CHA, LEV including Nu-3, MCM-22 and EU-1, preferably AEI or CHA, and having a silica-to-alumina ratio of about 10 to about 50, such as about 15 to about 40.

In a first emission treatment system embodiment, the emission treatment system comprises the NO_(x) adsorber catalyst of the invention and a catalysed soot filter (CSF). The NO_(x) adsorber catalyst is typically followed by (e.g. is upstream of) the catalysed soot filter (CSF). Thus, for example, an outlet of the NO_(x) adsorber catalyst is connected to an inlet of the catalysed soot filter.

A second emission treatment system embodiment relates to an emission treatment system comprising the NO_(x) adsorber catalyst of the invention, a catalysed soot filter (CSF) and a selective catalytic reduction (SCR) catalyst.

The NO_(x) adsorber catalyst is typically followed by (e.g. is upstream of) the catalysed soot filter (CSF). The catalysed soot filter is typically followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst. A nitrogenous reductant injector may be arranged between the catalysed soot filter (CSF) and the selective catalytic reduction (SCR) catalyst. Thus, the catalysed soot filter (CSF) may be followed by (e.g. is upstream of) a nitrogenous reductant injector, and the nitrogenous reductant injector may be followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst.

In a third emission treatment system embodiment, the emission treatment system comprises the NO_(x) adsorber catalyst of the invention, a selective catalytic reduction (SCR) catalyst and either a catalysed soot filter (CSF) or a diesel particulate filter (DPF).

In the third emission treatment system embodiment, the NO_(x) adsorber catalyst of the invention is typically followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst. A nitrogenous reductant injector may be arranged between the oxidation catalyst and the selective catalytic reduction (SCR) catalyst. Thus, the catalyzed monolith substrate may be followed by (e.g. is upstream of) a nitrogenous reductant injector, and the nitrogenous reductant injector may be followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst. The selective catalytic reduction (SCR) catalyst are followed by (e.g. are upstream of) the catalysed soot filter (CSF) or the diesel particulate filter (DPF).

A fourth emission treatment system embodiment comprises the NO_(x) adsorber catalyst of the invention and a selective catalytic reduction filter (SCRF™) catalyst. The NO_(x) adsorber catalyst of the invention is typically followed by (e.g. is upstream of) the selective catalytic reduction filter (SCRF™) catalyst.

A nitrogenous reductant injector may be arranged between the NO_(x) adsorber catalyst and the selective catalytic reduction filter (SCRF™) catalyst. Thus, the NO_(x) adsorber catalyst may be followed by (e.g. is upstream of) a nitrogenous reductant injector, and the nitrogenous reductant injector may be followed by (e.g. is upstream of) the selective catalytic reduction filter (SCRF™) catalyst.

When the emission treatment system comprises a selective catalytic reduction (SCR) catalyst or a selective catalytic reduction filter (SCRF™) catalyst, such as in the second to fourth exhaust system embodiments described hereinabove, an ASC can be disposed downstream from the SCR catalyst or the SCRF™ catalyst (i.e. as a separate monolith substrate), or more preferably a zone on a downstream or trailing end of the monolith substrate comprising the SCR catalyst can be used as a support for the ASC.

Another aspect of the invention relates to a vehicle. The vehicle comprises an internal combustion engine, preferably a diesel engine. The internal combustion engine preferably the diesel engine, is coupled to an emission treatment system of the invention.

It is preferred that the diesel engine is configured or adapted to run on fuel, preferably diesel fuel, comprises 50 ppm of sulfur, more preferably 15 ppm of sulfur, such as 10 ppm of sulfur, and even more preferably 5 ppm of sulfur.

The vehicle may be a light-duty diesel vehicle (LDV), such as defined in US or European legislation. A light-duty diesel vehicle typically has a weight of <2840 kg, more preferably a weight of <2610 kg. In the US, a light-duty diesel vehicle (LDV) refers to a diesel vehicle having a gross weight of 8,500 pounds (US lbs). In Europe, the term light-duty diesel vehicle (LDV) refers to (i) passenger vehicles comprising no more than eight seats in addition to the driver's seat and having a maximum mass not exceeding 5 tonnes, and (ii) vehicles for the carriage of goods having a maximum mass not exceeding 12 tonnes.

Alternatively, the vehicle may be a heavy-duty diesel vehicle (HDV), such as a diesel vehicle having a gross weight of >8,500 pounds (US lbs), as defined in US legislation.

A further aspect of the invention is a method of treating an exhaust gas from an internal combustion engine comprising contacting the exhaust gas with the NO_(x) adsorber catalyst as hereinbefore described. In preferred methods, the exhaust gas is a rich gas mixture. In further preferred methods, the exhaust gas cycles between a rich gas mixture and a lean gas mixture.

In some preferred methods of treating an exhaust gas from an internal combustion engine, the exhaust gas is at a temperature of about 100 to 300° C.

In further preferred methods of treating an exhaust gas from an internal combustion engine, the exhaust gas is contacted with one or more further emissions control devices, in addition to the NO_(x) adsorber catalyst as hereinbefore described. The emissions control device or devices is preferably downstream of the NO_(x) adsorber catalyst.

Examples of a further emissions control device include a diesel particulate filter (DPF), a lean NO_(x) trap (LNT), a lean NO_(x) catalyst (LNC), a selective catalytic reduction (SCR) catalyst, a diesel oxidation catalyst (DOC), a catalysed soot filter (CSF), a selective catalytic reduction filter (SCRF™) catalyst, an ammonia slip catalyst (ASC) and combinations of two or more thereof. Such emissions control devices are all well known in the art.

Some of the aforementioned emissions control devices have filtering substrates. An emissions control device having a filtering substrate may be selected from the group consisting of a diesel particulate filter (DPF), a catalysed soot filter (CSF), and a selective catalytic reduction filter (SCRF™) catalyst.

It is preferred that the method comprises contacting the exhaust gas with an emissions control device selected from the group consisting of a lean NO_(x) trap (LNT), an ammonia slip catalyst (ASC), diesel particulate filter (DPF), a selective catalytic reduction (SCR) catalyst, a catalysed soot filter (CSF), a selective catalytic reduction filter (SCRF™) catalyst, a cold start catalyst (dCSC™), and combinations of two or more thereof. More preferably, the emissions control device is selected from the group consisting of a diesel particulate filter (DPF), a selective catalytic reduction (SCR) catalyst, a catalysed soot filter (CSF), a selective catalytic reduction filter (SCRF™) catalyst, and combinations of two or more thereof. Even more preferably, the emissions control device is a selective catalytic reduction (SCR) catalyst or a selective catalytic reduction filter (SCRF™) catalyst.

When the method of the invention comprises contacting the exhaust gas with an SCR catalyst or an SCRF™ catalyst, then the method may further comprise the injection of a nitrogenous reductant, such as ammonia, or an ammonia precursor, such as urea or ammonium formate, preferably urea, into exhaust gas downstream of the NO_(x) adsorber catalyst and upstream of the SCR catalyst or the SCRF™ catalyst.

Such an injection may be carried out by an injector. The injector may be fluidly linked to a source (e.g. a tank) of a nitrogenous reductant precursor. Valve-controlled dosing of the precursor into the exhaust gas may be regulated by suitably programmed engine management means and closed loop or open loop feedback provided by sensors monitoring the composition of the exhaust gas.

Ammonia can also be generated by heating ammonium carbamate (a solid) and the ammonia generated can be injected into the exhaust gas.

Alternatively or in addition to the injector, ammonia can be generated in situ (e.g. during rich regeneration of a LNT disposed upstream of the SCR catalyst or the SCRF™ catalyst). Thus, the method may further comprise enriching of the exhaust gas with hydrocarbons.

The SCR catalyst or the SCRF™ catalyst may comprise a metal selected from the group consisting of at least one of Cu, Hf, La, Au, In, V, lanthanides and Group VIII transition metals (e.g. Fe), wherein the metal is supported on a refractory oxide or molecular sieve. The metal is preferably selected from Ce, Fe, Cu and combinations of any two or more thereof, more preferably the metal is Fe or Cu.

The refractory oxide for the SCR catalyst or the SCRF™ catalyst may be selected from the group consisting of Al₂O₃, TiO₂, CeO₂, SiO₂, ZrO₂ and mixed oxides containing two or more thereof. The non-zeolite catalyst can also include tungsten oxide (e.g. V₂O₅/WO₃/TiO₂, WO_(x)/CeZrO₂, WO_(x)/ZrO₂ or Fe/WO_(x)/ZrO₂).

It is particularly preferred when an SCR catalyst, an SCRF™ catalyst or a washcoat thereof comprises at least one molecular sieve, such as an aluminosilicate zeolite or a SAPO. The at least one molecular sieve can be a small, a medium or a large pore molecular sieve. By “small pore molecular sieve” herein we mean molecular sieves containing a maximum ring size of 8, such as CHA; by “medium pore molecular sieve” herein we mean a molecular sieve containing a maximum ring size of 10, such as ZSM-5; and by “large pore molecular sieve” herein we mean a molecular sieve having a maximum ring size of 12, such as beta. Small pore molecular sieves are potentially advantageous for use in SCR catalysts.

In the method of treating an exhaust gas of the invention, preferred molecular sieves for an SCR catalyst or an SCRF™ catalyst are synthetic aluminosilicate zeolite molecular sieves selected from the group consisting of AEI, ZSM-5, ZSM-20, ERI including ZSM-34, mordenite, ferrierite, BEA including Beta, Y, CHA, LEV including Nu-3, MCM-22 and EU-1, preferably AEI or CHA, and having a silica-to-alumina ratio of about 10 to about 50, such as about 15 to about 40.

In a first embodiment, the method comprises contacting the exhaust gas with the NO_(x) adsorber catalyst of the invention and a catalysed soot filter (CSF). The NO_(x) adsorber catalyst is typically followed by (e.g. is upstream of) the catalysed soot filter (CSF). Thus, for example, an outlet of the NO_(x) adsorber catalyst is connected to an inlet of the catalysed soot filter.

A second embodiment of the method of treating an exhaust gas relates to a method comprising contacting the exhaust gas with the NO_(x) adsorber catalyst of the invention, a catalysed soot filter (CSF) and a selective catalytic reduction (SCR) catalyst.

The NO_(x) adsorber catalyst is typically followed by (e.g. is upstream of) the catalysed soot filter (CSF). The catalysed soot filter is typically followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst. A nitrogenous reductant injector may be arranged between the catalysed soot filter (CSF) and the selective catalytic reduction (SCR) catalyst. Thus, the catalysed soot filter (CSF) may be followed by (e.g. is upstream of) a nitrogenous reductant injector, and the nitrogenous reductant injector may be followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst.

In a third embodiment of the method of treating an exhaust gas, the method comprises contacting the exhaust gas with the NO_(x) adsorber catalyst of the invention, a selective catalytic reduction (SCR) catalyst and either a catalysed soot filter (CSF) or a diesel particulate filter (DPF).

In the third embodiment of the method of treating an exhaust gas, the NO_(x) adsorber catalyst of the invention is typically followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst. A nitrogenous reductant injector may be arranged between the oxidation catalyst and the selective catalytic reduction (SCR) catalyst. Thus, the NO_(x) adsorber catalyst may be followed by (e.g. is upstream of) a nitrogenous reductant injector, and the nitrogenous reductant injector may be followed by (e.g. is upstream of) the selective catalytic reduction (SCR) catalyst. The selective catalytic reduction (SCR) catalyst are followed by (e.g. are upstream of) the catalysed soot filter (CSF) or the diesel particulate filter (DPF).

A fourth embodiment of the method of treating an exhaust gas comprises the NO_(x) adsorber catalyst of the invention and a selective catalytic reduction filter (SCRF™) catalyst. The NO_(x) adsorber catalyst of the invention is typically followed by (e.g. is upstream of) the selective catalytic reduction filter (SCRF™) catalyst.

A nitrogenous reductant injector may be arranged between the NO_(x) adsorber catalyst and the selective catalytic reduction filter (SCRF™) catalyst. Thus, the NO_(x) adsorber catalyst may be followed by (e.g. is upstream of) a nitrogenous reductant injector, and the nitrogenous reductant injector may be followed by (e.g. is upstream of) the selective catalytic reduction filter (SCRF™) catalyst.

When the emission treatment system comprises a selective catalytic reduction (SCR) catalyst or a selective catalytic reduction filter (SCRF™) catalyst, such as in the second to fourth method embodiments described hereinabove, an ASC can be disposed downstream from the SCR catalyst or the SCRF™ catalyst (i.e. as a separate monolith substrate), or more preferably a zone on a downstream or trailing end of the monolith substrate comprising the SCR catalyst can be used as a support for the ASC.

A further aspect of the invention is the use of a mixed dopant NO_(x) storage enhancer to improve the low temperature NO_(x) storage capacity of a support material, relative to an equivalent support material that does not contain the mixed dopant NO_(x) storage enhancer. This is advantageous because at low temperatures (typically below about 200° C.), the NO_(x) storage function of existing catalysts is typically inefficient and continues to be an area of catalyst development in need of improvement.

A further aspect of the invention is the use of a mixed dopant NO_(x) storage enhancer to improve the NO_(x) reduction activity of a support material during a rich purge, relative to an equivalent support material that does not contain the mixed dopant NO_(x) storage enhancer.

A further aspect of the invention is the use of a mixed dopant NO_(x) storage enhancer to improve the N₂ selectivity of a support material during a rich purge, relative to an equivalent support material that does not contain the mixed dopant NO_(x) storage enhancer. This is advantageous because a poorly selective catalyst can result in the formation of N₂O rather than N₂, which is itself a pollutant and hence is generally undesirable to be formed in emission treatment systems.

EXAMPLES

The invention will now be illustrated by the following non-limiting examples.

Materials

The materials were prepared according to the following general methods:

Method 1

A high surface area CeO₂ (surface area=156 m²g⁻¹) was impregnated to incipient wetness with the nitrate precursor of the respective metal oxide of the dopant(s) to be used. The resulting doped CeO₂ was dried at 110° C. overnight, followed by calcination in air at 500° C./2 h. The doped CeO₂ was then impregnated with a platinum salt to achieve a Pt loading of 1 wt %. The Pt-impregnated doped ceria was dried at 110° C. and then calcined in air at 500° C./2 h. Table 1 below lists the different catalysts prepared. For entry 1, no metal oxide dopant was used.

TABLE 1 Catalyst Dopants (mol %) 1 1Pt/CeO₂ — — 2 1Pt/Nd—CeO₂ Nd (10) — 3 1Pt/Nd—Sm—CeO₂ Nd (8) Sm (8) 4 1Pt/Gd—Pr—CeO₂ Gd (8) Pr (8) 5 1Pt/La—Sm—CeO₂ La (8) Sm (8) 6 1Pt/La—Sr—CeO₂ La (7) Sr (4) 7 1Pt/Sm—Sr—CeO₂ Sm (8) Sr (8) 8 1Pt/Ca—Sr—CeO₂ Ca (5) Sr (2) 9 1Pt/Mg—Sr—CeO₂ Mg (6) Sr (4)

Method 2 Pd

A high surface area CeO₂ (surface area=156 m²g⁻¹) was impregnated to incipient wetness with the nitrate precursor of the respective metal oxide of the dopant(s) to be used. The resulting doped CeO₂ was dried at 110° C. overnight, followed by calcination in air at 500° C./2 h. The doped CeO₂ was then impregnated with a palladium salt to achieve a Pd loading of 1 wt %. The Pd-impregnated doped ceria was dried at 110° C. and then calcined in air at 500° C./2 h. Table 2 below lists the different catalysts prepared. For entry 1, no metal oxide dopant was used.

TABLE 2 Catalyst Dopants (mol %) 1 1Pd/CeO₂ — — 2 1Pd/Nd—CeO₂ Nd (10) — 3 1Pd/Nd—Sm—CeO₂ Nd (8) Sm (8)

Method 3 Pt/Pd

A high surface area CeO₂ (surface area=156 m²g⁻¹) was impregnated to incipient wetness with the nitrate precursor of the respective metal oxide of the dopant(s) to be used. The resulting doped CeO₂ was dried at 110° C. overnight, followed by calcination in air at 500° C./2 h. The doped CeO₂ was then impregnated with a platinum salt and a palladium salt to achieve the loading shown in Table 3 below. The Pt/Pd-impregnated doped ceria was dried at 110° C. and then calcined in air at 500° C./2 h. Table 3 below lists the different catalysts prepared. For entry 1, no metal oxide dopant was used.

TABLE 3 Catalyst Dopants (mol %) 1 0.83Pt/0.17Pd/CeO₂ — — (5:1 Pt:Pd) 2 0.67Pt/0.33Pd/Nd—Sm—CeO₂ Nd (8) Sm (8) (2:1 Pt:Pd) 3 0.83Pt/0.17Pd/Nd—Sm—CeO₂ Nd (8) Sm (8) (5:1 Pt:Pd)

Experimental Results Storage Tests Example 1

The NO_(x) storage activity in air at 500° C. of each of the powdered catalyst materials obtained by the general methods above was evaluated in a gas mixture containing 60 ppm NO, 1500 ppm CO, 400 ppm C₃H₆, 10% O₂, 5% CO₂ and 5% H₂O, with the remainder of the gas being nitrogen, using 0.4 grams of each powder catalyst sieved to between 250<d<355 microns and at a volumetric gas flow rate of 2 liters per minute at a MHSV of 300 L·hr⁻¹·g⁻¹. During the test, the gas mixture was diverted from the catalyst for the first minute before being passed through the sample for 5 minutes at the storage temperature (100, 150 or 200° C.). This adsorption stage is followed by Temperature Programmed Desorption (TPD) at a ramping rate of 15° C./minute in the presence of the NO-containing gas until the bed temperature reaches about 270° C. Each catalyst material was then exposed to a reducing gas mixture (Lambda=0.93) for 15 s.

The amount of NO_(x) and other gases present in the gas mixture was measured using Fourier transform infrared (FTIR) spectroscopy. The NO_(x) storage, calculated as the amount of NO₂ stored per gram of catalyst during the 5 minute period, is shown in Table 4 below.

TABLE 4 NO₂ stored (mg/g) Catalyst 100° C. 150° C. 200° C. 1 1Pt/CeO₂ 0.65 0.49 2.23 2 1Pd/CeO₂ 2.15 1.26 0.82 3 1Pt/Nd—CeO₂ 0.98 1.14 2.50 4 1Pd/Nd—CeO₂ 2.03 2.00 1.56 5 1Pt/Nd—Sm—CeO₂ 1.14 2.01 3.20 6 1Pt/Gd—Pr—CeO₂ 1.03 1.41 3.00 7 1Pt/La—Sm—CeO₂ 0.92 1.74 2.50 8 1Pt/La—Sr—CeO₂ 1.03 1.46 2.66 9 1Pt/Sm—Sr—CeO₂ 1.90 1.41 2.80 10 1Pt/Ca—Sr—CeO₂ 0.92 1.03 2.36 11 1Pt/Mg—Sr—CeO₂ 0.65 1.06 2.01 12 1Pd/Nd—Sm—CeO₂ 1.89 2.13 1.56 13 0.67 Pt/0.33 Pd/Nd—Sm—CeO₂ 1.12 2.72 2.42 14 0.83 Pt/0.17 Pd/Nd—Sm—CeO₂ 0.89 1.62 2.90

From the results shown above in Table 4, it is clear that the doped CeO₂ materials, i.e. entries 3-14 in Table 4, generally store a higher amount of NO_(x) than the undoped materials, i.e. entries 1 and 2. It can also be seen that and the sample containing Nd—Sm (e.g. entry 5) had the highest storage capacity at 150 and 200° C., i.e. at relatively low temperatures. Notably, this mixed dopant sample showed greater NO₂ storage than the equivalent material containing Nd alone (entry 3), indicating a beneficial synergistic effect of including multiple dopants over a single dopant.

It can also be seen from the results shown in Table 4 that the same effect was observed for Pd-containing samples as for Pt-containing samples.

Example 2

The NO₂ stored at different temperatures for the Pt—Nd—Sm—CeO₂ sample for different loadings of Nd—Sm (relative to Pt—CeO₂) was also measured. The results are shown in Table 5 below.

TABLE 5 NO₂ stored (mg/g) Wt % Nd—Sm loading 100° C. 150° C. 200° C. 1 20 0.77 2.15 2.64 2 16 1.14 2.01 3.20 3 10 1.02 1.16 2.76 4 5 0.99 0.90 2.49

The results in Table 5 suggest that, in general, increasing the wt % loading of the NO_(x) storage enhancer (in this case Nd—Sm mixed dopant) increases the amount of NO₂ stored at 100, 150 and 200° C. Table 5 also shows, however, that at 200° C. the sample containing 16 wt % of Nd—Sm mixed dopant had higher storage than the equivalent sample containing 20 wt % Nd—Sm.

Example 3

The NO₂ stored at different temperatures for the Pt—Nd—Sm—CeO₂ sample for different loadings of Pt at a constant NO_(x) storage enhancer loading (16.3 wt % Nd—Sm) was measured. The results are shown in Table 6 below.

TABLE 6 NO₂ stored (mg/g) wt % Pt loading 100° C. 150° C. 200° C. 1 1 1.14 2.01 3.20 2 0.75 0.72 1.91 2.74 3 0.5 1.65 2.00 2.75

The results in Table 6 show that a Pt loading of greater than 0.5 wt %, e.g. 0.75 wt % or 1 wt %, is beneficial for enhancing NO₂ stored under the conditions tested.

Example 4

In use, during the rich purge at 270° C., some of the NO_(x) stored by a NO_(x) adsorber catalyst is released as NO or NO₂ and some is reduced to either N₂ or N₂O. It is desirable for the treatment of exhaust gases that the main product during the purge is N₂.

Table 7 below shows the selectivity (% of N₂ of total product N₂, N₂O, NO, NO₂) of NO_(x) conversion to N₂ by each catalyst during the reduction step.

TABLE 7 % Selectivity to N₂ during Purge Catalyst 100° C. 150° C. 200° C. 1 1Pt/CeO₂ 66 62 70 2 1Pt/Nd—CeO₂ 94 94 93 3 1Pt/Nd—Sm—CeO₂ 95 92 96 4 1Pt/Gd—Pr—CeO₂ 90 91 94 5 1Pt/La—Sm—CeO₂ 93 91 97 6 1Pt/La—Sr—CeO₂ 85 86 93 7 1Pt/Sm—Sr—CeO₂ 87 90 96 8 1Pt/Ca—Sr—CeO₂ 83 83 89 9 1Pt/Mg—Sr—CeO₂ 84 83 93

It can be seen from Table 7 that the samples containing a mixed dopant NO_(x) storage enhancer loading are significantly more selective for the production of N₂ during the rich purge than the undoped sample (entry 1). The Nd—Sm doped material (entry 3) is particularly selective for N₂ at 100, 150 and 200° C.

Example 5

The NO_(x) Storage Activity of the catalysts comprising a mixed dopant NO_(x) storage enhancer was also measured under cyclic oxidising (lean) and reducing (rich) conditions. The samples were first thermally aged in air at 800° C. for 24 hrs prior to measurements being taken. The gas mixture during the oxidising and reducing period is shown in Table 8 below.

TABLE 8 GAS Lean (Lambda = 2.30) Rich (Lambda = 0.95) O₂ 12%  1.3%   CO₂ 6% 6% H₂O 6% 6% NO 200 ppm 200 ppm C₃H₆ 200 ppm 1000 ppm CO 1500 ppm 21000 ppm H₂ 0 ppm 7500 ppm N₂ remainder remainder

The oxidising period of the test was 300 seconds and the reducing period 16 seconds. The weight of powder sample used was 0.4 grams sieved to between 250<d<355 microns and a volumetric gas flow rate of 2 litres per minute at a MHSV of 300 L*hr⁻¹*g⁻¹. The system was at an initial temperature of 150° C. During the test, the gas mixture was diverted from the catalyst for the first minute before being passed through the sample and cycling between the oxidising and reducing conditions for 3 complete cycles, finishing under the reducing condition. The sample temperature was then increased and the test repeated.

The effect of this cyclic conditioning on the NO_(x) storage activity of the catalysts comprising a NO_(x) storage enhancer at 250° C. is shown in FIG. 1. It is clear from the data shown in FIG. 1 that for all the catalysts, the extent of NO_(x) storage increases after the rich purge but the effect is more pronounced for the compositions comprising a mixed dopant NO_(x) storage enhancer.

Example 6

Table 9 shows the amount of NO_(x) stored on these aged catalysts at different temperatures. The difference in the extent of NO_(x) storage between the 1^(st) and 3^(rd) cycle indicates either the activation or deactivation (i.e. the sample was not purged sufficiently) during exposure to the rich phase of the test.

TABLE 9 150° C. 200° C. 250° C. 300° C. Catalyst 1^(st) 3^(rd) 1^(st) 3^(rd) 1^(st) 3^(rd) 1^(st) 3^(rd) 1Pt/CeO₂ 1.37 0.98 1.04 1.49 0.64 1.56 0.74 1.71 1Pt/Nd—CeO₂ 1.40 1.21 1.25 1.59 1.27 1.87 1.38 2.76 1Pt/Nd—Sm—CeO₂ 1.39 1.08 0.92 1.39 1.12 2.97 2.77 3.21

It is clear from the results shown in Table 9 that at the relatively low temperature of 150° C., the samples are deactivated due to an insufficient purge. However, above that temperature (e.g. at 200, 250 or 300° C.) the samples comprising a mixed dopant NO_(x) storage enhancer are activated to a greater extent than the undoped material.

Example 7

Further evidence of the beneficial effect of the mixed dopant NO_(x) storage enhancer on the activation of the Pt—CeO₂ catalyst material is also observed when these catalysts were first reduced at 300° C. at Lambda=0.95 for 5 minutes (rich gas mixture), before the cyclic tests.

FIG. 2 shows the NO_(x) concentration during the cyclic lean-rich test at 150° C. following the reduction of the aged samples. It can be seen that the catalyst containing Nd—Sm as a mixed dopant NO_(x) storage enhancer shows the highest storage activity.

Table 10 shows the amount of NO_(x) stored on these aged-reduced catalysts at different temperatures.

TABLE 10 150° C. 200° C. 250° C. Catalyst 1^(st) 3^(rd) 1^(st) 3^(rd) 1^(st) 3^(rd) 1Pt/CeO₂ 2.50 2.00 2.71 2.40 2.30 2.33 1Pt/Nd—CeO₂ 2.70 2.95 3.75 4.02 3.29 3.34 1Pt/Nd—Sm—CeO₂ 3.00 3.20 4.14 4.49 3.90 4.19

It can be seen from the results shown in Table 10 that all of the reduced samples have higher storage activity compared to the aged only samples (i.e. those shown in Table 1). However, the effect is more pronounced in the material comprising a mixed dopant NO_(x) storage enhancer.

A further improvement in the NO_(x) storage function is observed if the catalyst is reduced under more strongly reducing conditions at 300° C. Lambda=0.93 for 5 minutes. These results are shown in Table 11 below.

TABLE 11 150° C. 200° C. 250° C. Catalyst 1^(st) 3^(rd) 1^(st) 3^(rd) 1^(st) 3^(rd) 1Pt/CeO₂ 2.67 3.04 3.83 4.24 3.47 3.76 1Pt/Nd—CeO₂ 2.95 3.34 4.01 4.64 3.94 4.10 1Pt/Nd—Sm—CeO₂ 3.34 3.87 4.94 5.46 4.31 4.83

Example 8

1.24 g/in³ 10% Ce on 20% MgO/Al₂O₃Spinel is made into a slurry with distilled water and then milled to a d₉₀ of 13-15 μm. To the slurry, 100 g/ft³ Pt malonate and 20 g/ft³ Pd nitrate solution is then added, and stirred until homogenous. The Pt/Pd is allowed to adsorb onto the Spinel support for 1 hour.

To this is then added 3 g/in³ of either undoped CeO₂ or Nd—Sm—CeO₂ (prepared as described in Method 3 above) and 0.2 g/in³ alumina binder (Disperal), and stirred until homogenous to form a washcoat.

The washcoat is then coated onto a ceramic or metallic monolith using standard procedures, dried at 100° C. and calcined at 500° C. for 45 mins.

Each of the catalysts thus formed were performance tested over a simulated MVEG-B emissions cycle using a 1.6 litre bench mounted diesel engine. Emissions were measured pre- and post-catalyst.

The results from one representative cycle of the Engine Bench test are shown in Table 12 below.

TABLE 12 Time NOx Storage @80% Efficiency (g) (seconds) 1Pt/CeO₂ 1Pt/Nd—Sm—CeO₂ 150 0.27 0.46 175 0.26 0.58 200 0.23 1 250 0.09 0.9

It can be seen from the results in Table 12 that the catalyst comprising a mixed dopant NO_(x) storage enhancer stored significantly more NO_(x) at each time point at which a measurement was taken than the comparative undoped catalyst.

Example 9

Core samples were taken from each of the catalysts described in Example 8 above (i.e. 0.83Pt/0.17Pd/CeO₂ and 0.83Pt/0.17Pd/Nd—Sm—CeO₂). The cores were pre-conditioned by heating in a ramp to 400° C. in a gas mixture comprising 6% CO₂, 12% O₂ and balance N₂, followed by seven cycles of lean-rich preconditioning using the gas mixtures shown below in Table 13 (in each case the balance is nitrogen). The cycles were 120 seconds lean/10 seconds rich, at a space velocity (SV) of 40,000 h⁻¹.

TABLE 13 Lean Rich O₂ (%) 12 0.9 CO₂ (%) 6 10 H₂O (%) 6 12 NO (ppm) 200 100 C₃H₆ (ppm as C₁) 500 3000 CO (ppm) 1500 21000 H₂ (ppm) — 7500

Catalytic activity was determined using a synthetic gas bench test. The cores were tested in a simulated catalyst activity testing (SCAT) gas apparatus using the inlet gas mixture in Table 13. The test consisted of six cycles of 300 seconds lean/16 seconds rich.

The results from one representative cycle of the SCAT test at low SV (40,000 h⁻¹) at 200° C. are shown in Tables 14 and 15 below.

TABLE 14 Temperature NO_(x) Storage (g/L) (° C.) 1Pt/CeO₂ 1Pt/Nd—Sm—CeO₂ 150 0.1 0.3 175 0.1 0.5 200 0.2 0.8 250 0.6 1

It can be seen from the results in Table 14 that the catalyst comprising a mixed dopant NO_(x) storage enhancer stored significantly more NOx at each time point at which a measurement was taken than the comparative undoped catalyst.

TABLE 15 Temperature NO_(x) Conversion (%) (° C.) 1Pt/CeO₂ 1Pt/Nd—Sm—CeO₂ 150 4.6 11.4 175 2.6 23.2 200 17.8 28.3 250 40.1 52.8

It can be seen from the results in Table 15 that the NOx conversion of the catalyst comprising a mixed dopant NO_(x) storage enhancer was higher at all temperatures than the comparative undoped catalyst. 

1. A NO_(x) adsorber catalyst composition comprising a support material and one or more platinum group metals disposed on the support material; wherein the one or more platinum group metals is selected from the group consisting of palladium, platinum, or a mixture or alloy of platinum and palladium; wherein the support material comprises alumina, ceria, a ceria/zirconia mixed or composite oxide, or a magnesia/alumina mixed or composite oxide; and wherein the support material comprises a mixed dopant NO_(x) storage enhancer, wherein the mixed dopant NO_(x) storage enhancer comprises a plurality of elements selected from the group consisting of scandium, yttrium, lanthanum, praseodymium, neodymium, promethium, samarium, europium, gadolinium, terbium, dysprosium, holmium, erbium, thulium, ytterbium, lutetium, beryllium, magnesium, calcium, strontium, and radium, or metal oxides thereof.
 2. The NO_(x) adsorber catalyst composition of claim 1, wherein the mixed dopant NO_(x) storage enhancer is selected from a mixture of neodymium and samarium, gadolinium and praseodymium, lanthanum and samarium, lanthanum and strontium, samarium and strontium, calcium and strontium, or magnesium and strontium, or metal oxides thereof.
 3. The NO_(x) adsorber catalyst composition of claim 1, wherein the mixed dopant NO_(x) storage enhancer comprises a mixture of neodymium and samarium, or metal oxides thereof.
 4. The NO_(x) adsorber catalyst composition of claim 1, wherein the support material is selected from the group consisting of cerium oxide, a ceria-zirconia mixed oxide, a ceria-magnesia-alumina mixed oxide, and an alumina-ceria-zirconia mixed oxide.
 5. The NO_(x) adsorber catalyst composition of claim 1, further comprising barium.
 6. The NO_(x) adsorber catalyst composition of claim 1, wherein the NO_(x) adsorber catalyst composition is substantially free of barium.
 7. A NO_(x) adsorber catalyst comprising the NO_(x) adsorber catalyst composition of claim 1 supported on a metal or ceramic substrate.
 8. The NO_(x) adsorber catalyst of claim 7, wherein the substrate is a flow-through monolith or a filter monolith.
 9. The NO_(x) adsorber catalyst composition of claim 1, wherein the NO_(x) adsorber catalyst composition is extruded to form a flow-through or filter substrate.
 10. An emission treatment system for treating a flow of a combustion exhaust gas comprising an internal combustion engine and the NO_(x) adsorber catalyst of claim
 1. 11. The emission treatment system of claim 10, wherein the internal combustion engine is a diesel engine.
 12. The emission treatment system of claim 10, further comprising a selective catalytic reduction catalyst system, a particulate filter, a selective catalytic reduction filter system, a passive NO_(x) adsorber, a three-way catalyst system, or combinations thereof.
 13. A method for treating an exhaust gas from an internal combustion engine comprising contacting the exhaust gas with the NO_(x) adsorber catalyst of claim
 1. 14. The method of claim 13, wherein the exhaust gas is at a temperature of about 100 to 300° C.
 15. The method of claim 13, wherein the NO_(x) adsorber catalyst has a higher NO_(x) storage capacity relative to an equivalent support material that does not contain the NO_(x) storage enhancer.
 16. The method of claim 13 further comprising a rich purge step, wherein the NO_(x) adsorber catalyst has a higher NO_(x) reduction activity during the rich purge relative to an equivalent support material that does not contain the NO_(x) storage enhancer.
 17. The method of claim 13 further comprising a rich purge step, wherein the NO_(x) adsorber catalyst has a higher N₂ selectivity relative to an equivalent support material that does not contain the NO_(x) storage enhancer.
 18. The NO_(x) adsorber catalyst of claim 1, wherein the NO_(x) storage enhancer is present in an amount of about 0.5-20 mol. %, expressed as a total mol % of all of the components of the NO_(x) storage enhancer.
 19. The NO_(x) adsorber catalyst of claim 18, wherein the plurality of elements in the NO_(x) storage enhancer is two elements which are present in a mole ratio of from 1:10 to 10:1.
 20. The NO_(x) adsorber catalyst of claim 19, wherein the two elements are neodymium and samarium. 